|Número de publicación||US4349613 A|
|Tipo de publicación||Concesión|
|Número de solicitud||US 06/213,372|
|Fecha de publicación||14 Sep 1982|
|Fecha de presentación||5 Dic 1980|
|Fecha de prioridad||6 Dic 1979|
|También publicado como||DE2949011A1, DE2949011C2|
|Número de publicación||06213372, 213372, US 4349613 A, US 4349613A, US-A-4349613, US4349613 A, US4349613A|
|Cesionario original||Varta Batterie Aktiengesellschaft|
|Exportar cita||BiBTeX, EndNote, RefMan|
|Citas de patentes (5), Citada por (108), Clasificaciones (10), Eventos legales (1)|
|Enlaces externos: USPTO, Cesión de USPTO, Espacenet|
The invention relates to a method for electrochemical energy production from lithium high-energy cells having aqueous electrolytes and which operate in a combined system with hydrogen-oxygen fuel cells.
The further subject of the invention is a system which makes it possible to operate the combined system with a lithium high-energy cell and fuel cell, to which if appropriate a lead storage battery may also be added, with no loss and within an installation which is self-contained. Such an energy production installation of self-sufficient type is particularly suitable for ship propulsion.
Galvanic high-energy cells which operate on the basis of Li/H2 O or Li/H2 O2 are known from British Pat. No. 1,530,214. They consist of a highly reactive negative alkali metal electrode and a counter-electrode of inert metal, both of which are immersed in an aqueous electrolyte solution. As depolarizers at the counter-electrode, oxygen, hydrogen peroxide, or even water may be used. Special measures such as the creation of porous cover layers upon the negative electrode are taken in order to prevent an excessively strong effect of on and heat production.
If one considers an Li/H2 O2 cell, the actual current producing reaction is given by the expression
Li+1/2H.sub.2 O.sub.2 →LiOH (+heat+electrical energy). (1)
At the same time parasitic reactions take place which are not electrochemically effective, namely
Li+2H.sub.2 O→LiOH×H.sub.2 O+1/2H.sub.2 (corrosion), (2)
H.sub.2 O.sub.2 →H.sub.2 O+1/2O.sub.2 (Decomposition) 3)
If no oxidant such as H2 O2 or O2 is present then H2 O is obliged to be the depolarizer and the reduction of the water liberates additional hydrogen.
H.sub.2 O+e.sup.- →OH.sup.- +1/2H.sub.2 ( 4)
The operation of an aqueous galvanic high-energy cell is therefore not problem free. Nevertheless, intensive efforts are currently underway to open up for the above-mentioned electrochemical system suitable fields of use, e.g. as the energy source for ship propulsion. The theoretical rest potential of an Li/H2 O2 cell indeed amounts to 3.93 volts and the energy density relative to lithium is 15,150 Wh/kg.
Accordingly, it has already been proposed in co-pending U.S. patent application Ser. No. 122,612, filed Feb. 19, 1980, which is assigned to the same assignee as the present application to decompose the H2 /O2 gas mixture which unavoidably evolves in lithium high-energy cells into its components, and to supply these to a fuel cell in order to utilize the recombination energy inherent therein. According to this proposal, the gas mixture, if appropriate with the addition of oxygen, is supplied to the positive electrode of a fuel cell. From there, if appropriate with separation of excess oxygen, it is further ducted to the negative electrode of the fuel cell and is recombined into water with simultaneous production of electrical energy. The type of fuel cell which is particularly suitable for this recombination is the low pressure oxyhydrogen gas cell. It utilizes in its modern embodiments a positive electrode of sintered nickel with a special catalyst for the oxygen reduction. As negative electrode for the oxidation of the hydrogen there is suitable, for example, a double skeleton catalyst electrode of the type described in German Pat. No. 1,019,361 which is sintered from carbonyl nickel and highly active Raney-nickel powder. Both electrodes are respectively preceded by a gas space for the supply and distribution of the hydrogen or oxygen. The electrolyte, which is positioned between the double skeleton electrodes, is preferably caused to circulate.
In addition to these fuel cell electrodes, there are also in use other, pressure free working electrodes based upon nickel nets and catalyzed carbon powder, cf. A. Winsel in Ullmanns Encyklopadie der techn. Chemie, (English translation: Encylopedia of Technical Chemistry) Volume 12, p. 113 et seq. (1976).
Basically, one can proceed in such a manner that the gas mixture exiting from the lithium cell is supplied first to the O2 electrode of the fuel cell where the oxygen is largely removed and the remaining gas then enters the H2 electrode of the fuel cell. The operation of the fuel cell permits an electrochemical transformation of H2 and O2 only in the stoichiometric relationship of water. If H2 is present in excess, this excess remains untransformed and must be expelled at the end of the fuel cell like an inert gas. If on the other hand O2 is present in excess, this excess oxygen also enters the H2 electrode of the fuel cell. It is a property of all H2 electrodes that they also simultaneously electrochemically transform O2 in short-circuit. In that case an O2 excess is co-consumed in the H2 electrode. This characteristic has a lowering effect upon the efficiency of the electrochemical energy transformation of the gas mixture in the fuel cell.
In a preferred embodiment of the proposed method, precautions are therefore taken with the object of supplying to the fuel cell the operating gases hydrogen and oxygen in an optimal relationship, namely in the stoichiometric relationship of water.
In the case of an H2 excess this is done most simply by introducing into the gas mixture which flows to the O2 electrode additional air, or O2, which may, for example, stem from the decomposition of peroxide.
Alternatively, in the case of an O2 excess, the O2 is separated from the gas mixture so that only pure H2 reaches the negative fuel cell electrode. In accordance with the invention a particularly suitable means for this separation has proven to be an electrochemical cell which functions on the principle of an O2 /O2 gas chain and operates as "cleaning cell."
Lithium hydroxide which evolves in a lithium high-energy cell possesses limited solubility and therefore requires, if one wishes to store it for lithium recovery, a large volume because of the dilution water. However, through entrainment of liquid carbon dioxide, the lithium hydroxide may be bound into lithium carbonate and the solvent water which is thereby liberated can be returned to the circulation of the Li/H2 O2 cell. In this manner, carbon dioxide is stored in the stoichiometric relationship of the lithium carbonate for use by the energy supply installation. However, in this process, the energy of neutralization is lost to the electrochemical energy production process through transformation into heat.
Accordingly, it is an object of the invention to provide a carbon dioxide source for neutralizing the lithium hydroxide created in the lithium cells. This source is supplied with carbon compounds, which contain the carbon in as reduced a form as possible, so that they can be made useful for the production of additional energy.
This and other objects which will appear are accomplished in accordance with the invention by reacting the lithium hydroxide, which forms during the cell reaction in the lithium cell, with a carbon dioxide to produce lithium carbonate. This is produced in a reformer from hydrocarbons or hydrocarbon compounds and water. The simultaneously produced hydrogen gas is supplied to the fuel cell.
The reforming of hydrocarbons or hydrocarbon compounds in accordance with the invention can be combined very appropriately with the current delivery from lithium high energy cells, if there is timely present as much carbon dioxide from the reformer as is required to neutralize the lithium hydroxide produced in the lithium cell.
In the particularly desirable methanol reforming method according to reaction formula (5) presented below, there are produced in the presence of a catalyst in endothermic reaction simultaneously 1 mole of carbon dioxide and 3 moles of hydrogen gas per mole of methanol. The hydrogen gas can be supplied to a fuel cell for the production of electrochemical energy. An additional mole of hydrogen is added when the lithium high energy cell is operated as a lithium/water cell in accordance with the reaction formula (6), in which the 2-g atoms of lithium become 2 moles of lithium hydroxide, which are united into lithium carbonate by the carbon dioxide which is produced stoichiometrically from 1 mole of methanol in accordance with the reaction formula (5).
As a reaction partner for the hydrogen in the fuel cell, oxygen can be produced, for example, from liquefied oxygen, but preferably according to the reaction formula (7) through hydrogen peroxide decomposition, so that the overall reaction formula (8) applies for the overall process. ##STR2##
The volume of the substances on the left side and their weights determine the energy weight of the reaction substances for the process.
If the reaction formula (8) is used, it must be noted that this is an overall reaction. The process technology, however, requires that the hydrogen peroxide be stored in, for example, 70% by weight form, so that the overall reaction expression (9) has to be considered for practical use:
2Li+CH.sub.3 OH+4(H.sub.2 O.sub.2 +0.81H.sub.2 O)→Li.sub.2 CO.sub.3 +9.24H.sub.2 O (9)
For such as system there are obtained as the theoretical energy density the following values:
Realizable electrical energy at 1.9 V cell potential in the Li/H2 O cell per formula transformation
E.sub.1 =102 Wh,
at 0.8 cell potential in the fuel cell
E.sub.2 =171 Wh,
Relative to the weight of the stored reaction substances per formula G=240 g, i.e. at the volume of V=216 cm3, the important specific values, without taking the transformations into account are
The reaction heat ΔH, which is created by the reaction according to formula (9) is
ΔH=516 Wh per formula transformation.
Accordingly the efficiency is
For the practical performance of the process embodying the invention, there is provided apparatus which includes in combination the following essential elements: a lithium high energy cell with aqueous electrolyte, followed by a hydrogen/oxygen fuel cell, a reformer for obtaining hydrogen/carbon dioxide mixtures from hydrocarbons or hydrocarbon compounds and for neutralizing the lithium hydroxide of the lithium cell by means of the carbon dioxide in the reformer gas, and a gas washing device.
For further details, reference is made to the discussion which follows, in light of the accompanying drawings, wherein:
FIG. 1 shows the installation in diagrammatic form, by means of which the raw material and energy flow can be visualized.
FIG. 2 shows the details of the reformer.
As illustrated in FIG. 1, the lithium tank 1, the methanol tank 2 and the hydrogen peroxide tank 3 contain the raw materials. The lithium is caused to electrochemically react in the lithium cell 4 together with H2 O from an H2 O reservoir 5. An apparatus suitable for this purpose is known (cf. E. L. Littauer, W. R. Momeyer and K. C. Tsai, Journal of Power Sources 2 (1977/78), pages 163-176).
The reaction in the lithium/H2 O cell is characterized by heat loss, which can be seen from the fact that, in lieu of the theoretical potential of 2.23 V for the lithium/H2 O cell, one can count only on a load potential of 1.9 V. For the removal of this heat, as well as for matching the electrolyte flow to the output required from the cell, the lithium/H2 O cell is provided with electrolyte circulation. In addition, to remove the lithium hydroxide reaction product, water, also from H2 O reservoir 5, must be supplied and concentrated LiOH solution must be removed.
This excess solution is supplied to a gas washer 6 in accordance with the invention, and is there brought into contact with the hydrogen/carbon dioxide mixture produced in reformer 7. This produces pure hydrogen and lithium carbonate which settles out in the gas washer 6 and remains there, whereas the separated water is returned to the H2 O reservoir 5. After passing through the gas washer 6 the hydrogen is, if appropriate, stored in a metal hydride reservoir 8 or in a pressure flask or in the low pressure piping itself, before being supplied to the fuel cell 9.
The oxygen for the fuel cell is derived from the hydrogen peroxide tank 3 via the H2 O2 decomposer 10 and the O2 reservoir 11.
Such a combined electrochemical energy supply system can be operated completely self-sufficiently without supply or removal of reagent. It is therefore particularly suitable for submarine travel or for energy supply installations in similar situations.
As appears from the diagram of FIG. 1, it is possible to temporarily remove the lithium cell from the working combination and to maintain only the fuel cell in operation for current supply. The fuel cell is then alone supplied with hydrogen from the reformer 7 and oxygen from the H2 O2 decomposer 10. However, over extended periods, the operating stages and the overall material transformation in the installation should be so matched to each other that the stoichiometry of the overall reaction formula (8) or (9) is met.
In FIG. 1 there is further indicated the possibility of parallel operation of lithium cell and fuel cell with a storage battery 12. For load equilization of the current sources among themselves, as well as for load control of motor 13, regulators 14 are provided.
In contrast to the reaction (6) in the lithium cell, the reaction (5) in the reformer is endothermic, i.e. a gas mixture is produced from methanol and water which consumes 16.25 Wh/formula of heat. As is seen from expression (5), the gas volume doubles during the reaction in the reformer, i.e. the reaction is accompanied by a swelling flow and this again indicates that it can occur only in thin layers of the catalyst. Of course this reaction proceeds the better the less resistance is met by the flow of the reaction heat to the place of reaction. It has been found that this reaction proceeds especially well with catalysts which contain copper chromite embedded in a copper frame, in the manner of a double skeleton structure and pressed, or rolled, or possibly sintered upon a sheet-like carrier.
The reverse side of this plate serves to supply the heat and this can be accomplished advantageously, for example, in that the reverse side is provided with a recombination mat for hydrogen and oxygen and an oxyhydrogen gas mixture is permitted to react there. It is particularly desirable if the very pure hydrogen from the lithium/water cell is used for this purpose and, for example, the recombination gas is controlled by the temperature of the reformer 7. A desirable structure for this purpose involves a register-like arrangement of plates 14 according to FIG. 2 in which two reformer layers 15 in confronting position define the reforming space 16 and two recombination catalysts 17 in confronting position define the recombination space 18.
In place of the recombination heat of the hydrogen/oxygen mixture, the heat can also be obtained from the decomposition heat of the hydrogen peroxide of 110 Wh per formula quantity in formula (3). For this purpose there is brought into thermal contact the hot O2 gas from the catalytic H2 O2 decomposer 10 with the reforming catalyst of the reformer layers 15, or, the recombination space 18 is made into a decomposition space for hydrogen peroxide of such configuration that the reverse sides of the reforming catalyst bearing plates 14 contain a layer which is catalytically effective for the hydrogen peroxide decomposition. Catalytically effective in this sense are, for example, MnO2 or silver catalyst particles which have been embedded in a porous sintered nickel layer, or in the manner of the double skeleton (DSK) process. Here, too, it is desirable to a hydrogen reservoir in-between because, although all the reactions in this process take place in suitable sequence, it is desirable to provide the possibility of phase displacement through the in-between connection of reservoirs.
To the extent that, in place of the preferred methanol, higher alcohols as well as cyclic and aliphatic carbohydrates can be made useful as hydrogen sources by a reforming process, this applies only with the limitation that the reforming temperatures for long chain hydrocarbons are substantially higher. On the other hand, in these cases a higher density is obtained during storage.
Further heat utilization is possible by using the heat for the evaporation and preheating of the reformer mixture consisting, for example, of methanol and water.
The previously mentioned values for energy density apply without the various energy transformers. There, weight and volume are again dependent upon the required output. The specific values for the overall aggregate become optimal when the Li/H2 O cell, the methanol reformer, and the fuel cell are adjusted for medium performance and when peak performance is obtained by combination thereof with a lead storage battery. This method of operation corresponds to the diagrammatic illustration of FIG. 1.
In hydrogen peroxide, the hydrogen is stored with high density. It can also be readily split off from this compound and supplied via a piping system to the fuel cell and if appropriate, to the lithium cell provided their cathodes are constructed as oxygen cathodes. However, instead of from the hydrogen peroxide, the installation can also be supplied with oxygen from a liquefied gas, cold evaporator, the automatic matching of the gasification performance to the demand being within the state of the art.
If the Li/water cell is operated with a hydrogen cathode instead of an oxygen cathode, then its useful voltage is about 0.7 V higher. On the other hand, the corresponding energy yield detracts from the reaction in the fuel cell, which now has available only the hydrogen from the reformer and the relatively small quantity of hydrogen which was formed parasitically at the Li anode without current production. The fuel cell can then indeed be made somewhat smaller, but this is at the expense of a complicated reaction process in the Li/H2 O cell.
|Patente citada||Fecha de presentación||Fecha de publicación||Solicitante||Título|
|US3338746 *||24 Abr 1964||29 Ago 1967||Bbc Brown Boveri & Cie||Low-temperature fuel cell in combination with a power accumulator|
|US3539395 *||25 Feb 1966||10 Nov 1970||Gen Electric||System and process for the indirect electrochemical combination of air and a reformable fuel|
|US4081693 *||18 Jul 1975||28 Mar 1978||Stone Gordon R||Vehicular propulsion system|
|US4084038 *||1 Abr 1975||11 Abr 1978||Scragg Robert L||Electrical power generation and storage system|
|JPS5169132A *||Título no disponible|
|Patente citante||Fecha de presentación||Fecha de publicación||Solicitante||Título|
|US4677040 *||21 Feb 1986||30 Jun 1987||Gould Inc.||Power generation systems and methods|
|US4709882 *||25 Nov 1983||1 Dic 1987||Lockheed Missiles & Space Company, Inc.||Electric propulsion system for aircraft|
|US4756979 *||18 Jun 1986||12 Jul 1988||Gould Inc.||Power generation systems and methods|
|US4772634 *||31 Jul 1986||20 Sep 1988||Energy Research Corporation||Apparatus and method for methanol production using a fuel cell to regulate the gas composition entering the methanol synthesizer|
|US5141823 *||4 Mar 1985||25 Ago 1992||Vickers Shipbuilding And Engineering Limited||Electrical generating plant|
|US5401589 *||22 Nov 1991||28 Mar 1995||Vickers Shipbuilding And Engineering Limited||Application of fuel cells to power generation systems|
|US5527632 *||5 May 1995||18 Jun 1996||Rolls-Royce And Associates Limited||Hydrocarbon fuelled fuel cell power system|
|US6376113||12 Nov 1998||23 Abr 2002||Idatech, Llc||Integrated fuel cell system|
|US6383670||6 Oct 1999||7 May 2002||Idatech, Llc||System and method for controlling the operation of a fuel processing system|
|US6451464||3 Ene 2000||17 Sep 2002||Idatech, Llc||System and method for early detection of contaminants in a fuel processing system|
|US6485851 *||23 Sep 1998||26 Nov 2002||California Institute Of Technology||Power generation in fuel cells using liquid methanol and hydrogen peroxide|
|US6495277||26 Jul 2000||17 Dic 2002||Idatech, Llc||Fuel cell system controller|
|US6537352||19 Dic 2001||25 Mar 2003||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US6632270||20 Feb 2003||14 Oct 2003||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US6719831||5 May 2003||13 Abr 2004||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US6723156||5 May 2003||20 Abr 2004||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US6783741||20 Abr 2001||31 Ago 2004||Idatech, Llc||Fuel processing system|
|US6811908||3 May 2002||2 Nov 2004||Idatech, Llc||System and method for controlling the operation of a fuel processing system|
|US6818335||16 Sep 2002||16 Nov 2004||Idatech, Llc||System and method for early detection of contaminants in a fuel processing system|
|US6824593||5 Dic 2003||30 Nov 2004||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US6835481||22 Mar 2001||28 Dic 2004||Idatech, Llc||Fuel cell system with load management|
|US6869707||19 Abr 2002||22 Mar 2005||Idatech, Llc||Integrated fuel cell system|
|US6890672||26 Jun 2001||10 May 2005||Idatech, Llc||Fuel processor feedstock delivery system|
|US6979507||25 Nov 2002||27 Dic 2005||Idatech, Llc||Fuel cell system controller|
|US6994927||18 Mar 2005||7 Feb 2006||Idatech, Llc||Integrated fuel cell system|
|US7008708||10 Nov 2004||7 Mar 2006||Idatech, Llc||System and method for early detection of contaminants in a fuel processing system|
|US7052530||15 Nov 2004||30 May 2006||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US7128769||20 Jun 2003||31 Oct 2006||Idatech, Llc||Methanol steam reforming catalysts, steam reformers, and fuel cell systems incorporating the same|
|US7195663||25 May 2006||27 Mar 2007||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US7208241||15 Oct 2004||24 Abr 2007||Idatech, Llc||System and method for controlling the operation of a fuel processing system|
|US7250231||9 Jun 2003||31 Jul 2007||Idatech, Llc||Auxiliary fuel cell system|
|US7282291||24 Nov 2003||16 Oct 2007||California Institute Of Technology||Water free proton conducting membranes based on poly-4-vinylpyridinebisulfate for fuel cells|
|US7368194||6 May 2005||6 May 2008||Idatech, Llc||Fuel processor feedstock delivery system|
|US7368195||6 Mar 2006||6 May 2008||Idatech, Llc||System and method for early detection of contaminants in a fuel processing system|
|US7390587||3 Dic 2004||24 Jun 2008||Idatech, Llc||Fuel cell system with load management|
|US7410531||20 Mar 2007||12 Ago 2008||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US7470293||31 Mar 2005||30 Dic 2008||Idatech, Llc||Feedstock delivery systems, fuel processing systems, and hydrogen generation assemblies including the same|
|US7491458 *||14 Abr 2004||17 Feb 2009||Polyplus Battery Company||Active metal fuel cells|
|US7601302||16 Sep 2005||13 Oct 2009||Idatech, Llc||Self-regulating feedstock delivery systems and hydrogen-generating fuel processing assemblies and fuel cell systems incorporating the same|
|US7662195||23 Jun 2006||16 Feb 2010||Idatech, Llc||Methanol steam reforming catalysts, steam reformers, and fuel cell systems incorporating the same|
|US7682718||5 May 2008||23 Mar 2010||Idatech, Llc||Fuel processor feedstock delivery system|
|US7736404||22 Oct 2009||15 Jun 2010||Idatech, Llc||Methanol steam reforming catalysts, steam reformers, and fuel cell systems incorporating the same|
|US7736596||6 Oct 2009||15 Jun 2010||Idatech, Llc||Self-regulating feedstock delivery systems and hydrogen-generating fuel processing assemblies and fuel cell systems incorporating the same|
|US7754361||30 May 2007||13 Jul 2010||Idatech, Llc||Fuel cell systems with maintenance hydration by displacement of primary power|
|US7771882||19 Abr 2007||10 Ago 2010||Idatech, Llc||System and method for controlling the operation of a fuel processing system|
|US7789941||20 Abr 2009||7 Sep 2010||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US7819955||11 Ago 2008||26 Oct 2010||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US7842428||28 May 2004||30 Nov 2010||Idatech, Llc||Consumption-based fuel cell monitoring and control|
|US7846569||21 Dic 2005||7 Dic 2010||Idatech, Llc||Methods for operating a fuel cell system under reduced load conditions|
|US7887958||10 May 2007||15 Feb 2011||Idatech, Llc||Hydrogen-producing fuel cell systems with load-responsive feedstock delivery systems|
|US7939051||21 May 2007||10 May 2011||Idatech, Llc||Hydrogen-producing fuel processing assemblies, heating assemblies, and methods of operating the same|
|US7939211||9 Ago 2010||10 May 2011||Idatech, Llc||System and method for controlling the operation of a fuel processing system|
|US7972420||18 May 2007||5 Jul 2011||Idatech, Llc||Hydrogen-processing assemblies and hydrogen-producing systems and fuel cell systems including the same|
|US7985510||18 Abr 2005||26 Jul 2011||Idatech, Llc||Utilization-based fuel cell monitoring and control|
|US8021446||13 Sep 2006||20 Sep 2011||Idatech, Llc||Self-regulating feedstock delivery systems and hydrogen-generating fuel processing assemblies and fuel cell systems incorporating the same|
|US8034494||30 Jun 2010||11 Oct 2011||Idatech, Llc||Fuel cell systems with maintenance hydration by displacement of primary power|
|US8057575||21 Oct 2010||15 Nov 2011||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US8133626||3 Dic 2010||13 Mar 2012||Idatech, Llc||Fuel cell system controller|
|US8157900||9 Jun 2011||17 Abr 2012||Idatech, Llc||Hydrogen-processing assemblies and hydrogen-producing systems and fuel cell systems including the same|
|US8257466||14 Nov 2011||4 Sep 2012||Idatech, Llc||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US8262752||21 Oct 2008||11 Sep 2012||Idatech, Llc||Systems and methods for reliable feedstock delivery at variable delivery rates|
|US8277997||29 Jul 2004||2 Oct 2012||Idatech, Llc||Shared variable-based fuel cell system control|
|US8518568||13 Sep 2007||27 Ago 2013||Johnson Controls Technology Company||Battery system|
|US8563188||7 Mar 2012||22 Oct 2013||Idatech, Llc||Fuel cell system controller|
|US8608814||7 Sep 2012||17 Dic 2013||Dcns Sa||Systems and methods for reliable feedstock delivery at variable delivery rates|
|US8617754||9 Dic 2011||31 Dic 2013||Dcns Sa||Systems and methods for independently controlling the operation of fuel cell stacks and fuel cell systems incorporating the same|
|US8632898||28 Oct 2004||21 Ene 2014||Johnson Controls Technology Company||Battery system including batteries that have a plurality of positive terminals and a plurality of negative terminals|
|US8636828||29 Ago 2012||28 Ene 2014||Dcns Sa||Hydrogen purification membranes, components and fuel processing systems containing the same|
|US9515334||24 Jun 2011||6 Dic 2016||Dcns||Utilization-based fuel cell monitoring and control|
|US20020114984 *||13 Ago 2001||22 Ago 2002||Edlund David J.||Fuel cell system with stored hydrogen|
|US20020127447 *||3 May 2002||12 Sep 2002||Edlund David J.||System and method for controlling the operation of a fuel processing system|
|US20030008186 *||26 Jun 2001||9 Ene 2003||Dickman Anthony J.||Fuel processor feedstock delivery system|
|US20030017374 *||16 Sep 2002||23 Ene 2003||Edlund David J.||System and method for early detection of contaminants in a fuel processing system|
|US20030113601 *||25 Nov 2002||19 Jun 2003||Edlund David J.||Fuel cell system controller|
|US20030167690 *||3 Mar 2003||11 Sep 2003||Edlund David J.||Feedstock delivery system and fuel processing systems containing the same|
|US20030175563 *||11 Mar 2003||18 Sep 2003||Rolf Bruck||Fuel cell facility and method for operating a fuel cell facility|
|US20040006915 *||20 Jun 2003||15 Ene 2004||Curtiss Renn||Methanol steam reforming catalysts, steam reformers, and fuel cell systems incorporating the same|
|US20040081867 *||23 Oct 2002||29 Abr 2004||Edlund David J.||Distributed fuel cell network|
|US20040081868 *||6 Nov 2002||29 Abr 2004||Edlund David J.||Distributed fuel cell network|
|US20040247961 *||9 Jun 2003||9 Dic 2004||Edlund David J.||Auxiliary fuel cell system|
|US20050064253 *||10 Nov 2004||24 Mar 2005||Edlund David J.||System and method for early detection of contaminants in a fuel processing system|
|US20050084726 *||3 Dic 2004||21 Abr 2005||Dickman Anthony J.||Fuel cell system with load management|
|US20050100792 *||14 Abr 2004||12 May 2005||Polyplus Battery Company||Active metal fuel cells|
|US20050106431 *||15 Oct 2004||19 May 2005||Edlund David J.||System and method for controlling the operation of a fuel processing system|
|US20050174092 *||28 Oct 2004||11 Ago 2005||Johnson Controls Technology Company||Battery system|
|US20050181248 *||18 Mar 2005||18 Ago 2005||Edlund David J.||Integrated fuel cell system|
|US20050266284 *||28 May 2004||1 Dic 2005||Mesa Scharf||Consumption-based fuel cell monitoring and control|
|US20050266285 *||18 Abr 2005||1 Dic 2005||Edlund David J||Utilization-based fuel cell monitoring and control|
|US20060024540 *||29 Jul 2004||2 Feb 2006||Laven Arne||Shared variable-based fuel cell system control|
|US20060076535 *||14 Nov 2005||13 Abr 2006||Oroskar Anil R||Process for the production of hydrogen|
|US20060090396 *||31 Mar 2005||4 May 2006||Edlund David J||Feedstock delivery systems, fuel processing systems, and hydrogen generation assemblies including the same|
|US20060134473 *||21 Dic 2005||22 Jun 2006||Edlund David J||Fuel cell system controller|
|US20060154120 *||6 Mar 2006||13 Jul 2006||Edlund David J||System and method for early detection of contaminants in a fuel processing system|
|US20060236607 *||23 Jun 2006||26 Oct 2006||Curtiss Renn||Methanol steam reforming catalysts, steam reformers, and fuel cell systems incorporating the same|
|US20070042233 *||14 Abr 2006||22 Feb 2007||Lyman Scott W||Systems and methods for initiating auxiliary fuel cell system operation|
|US20070275275 *||11 May 2007||29 Nov 2007||Mesa Scharf||Fuel cell anode purge systems and methods|
|US20080176118 *||19 Abr 2007||24 Jul 2008||Edlund David J||System and method for controlling the operation of a fuel processsing system|
|US20080220315 *||13 Sep 2007||11 Sep 2008||Johnson Controls Technology Company||Battery system|
|US20080248347 *||5 May 2008||9 Oct 2008||Idatech, Llc||Fuel processor feedstock delivery system|
|US20080299420 *||30 May 2007||4 Dic 2008||Kelley Mason P||Fuel cell systems with maintenance hydration by displacement of primary power|
|US20080299423 *||30 May 2007||4 Dic 2008||Laven Arne||Fuel cell systems with maintenance hydration|
|US20100040918 *||22 Oct 2009||18 Feb 2010||Idatech, Llc||Methanol steam reforming catalysts, steam reformers, and fuel cell systems incorporating the same|
|US20110033765 *||21 Oct 2010||10 Feb 2011||Idatech, Llc||Consumption-based fuel cell monitoring and control|
|DE10008823B4 *||25 Feb 2000||17 Ago 2006||Nucellsys Gmbh||Brennstoffzellensystem und Verfahren zum Betrieb eines Brennstoffzellensystems|
|EP1217678A2 *||30 Nov 2001||26 Jun 2002||Volkswagen Aktiengesellschaft||Fuel cell system with intermediate storage device and control method|
|EP1217678A3 *||30 Nov 2001||9 Jun 2004||Volkswagen Aktiengesellschaft||Fuel cell system with intermediate storage device and control method|
|WO2002019789A2 *||7 Sep 2001||14 Mar 2002||Emitec Gesellschaft Für Emissionstechnologie Mbh||Fuel cell device and method for operating a fuel cell device|
|WO2002019789A3 *||7 Sep 2001||5 Dic 2002||Emitec Emissionstechnologie||Fuel cell device and method for operating a fuel cell device|
|Clasificación de EE.UU.||429/424, 429/499, 429/425, 429/441|
|Clasificación internacional||H01M8/06, H01M16/00|
|Clasificación cooperativa||H01M8/0612, H01M16/006|
|Clasificación europea||H01M16/00F2, H01M8/06B2|
|27 Feb 1981||AS||Assignment|
Owner name: VARTA BATTERIE, A.G. 3000 HANNOVER 2L, AM LEINEUFE
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:WINSEL AUGUST;REEL/FRAME:003833/0951
Effective date: 19801121